EP0008770A1 - Installation pour l'élimination de substances gazeuses nocives des gaz de combustion - Google Patents

Installation pour l'élimination de substances gazeuses nocives des gaz de combustion Download PDF

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Publication number
EP0008770A1
EP0008770A1 EP79103191A EP79103191A EP0008770A1 EP 0008770 A1 EP0008770 A1 EP 0008770A1 EP 79103191 A EP79103191 A EP 79103191A EP 79103191 A EP79103191 A EP 79103191A EP 0008770 A1 EP0008770 A1 EP 0008770A1
Authority
EP
European Patent Office
Prior art keywords
additives
cascades
pipe
cascade
metering
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Granted
Application number
EP79103191A
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German (de)
English (en)
Other versions
EP0008770B1 (fr
Inventor
Gerhard Dipl.-Ing. Kritzler
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Apparatebau Rothemuehle Brandt and Kritzler GmbH
Original Assignee
Apparatebau Rothemuehle Brandt and Kritzler GmbH
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Apparatebau Rothemuehle Brandt and Kritzler GmbH filed Critical Apparatebau Rothemuehle Brandt and Kritzler GmbH
Publication of EP0008770A1 publication Critical patent/EP0008770A1/fr
Application granted granted Critical
Publication of EP0008770B1 publication Critical patent/EP0008770B1/fr
Expired legal-status Critical Current

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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/46—Removing components of defined structure
    • B01D53/48—Sulfur compounds
    • B01D53/50—Sulfur oxides
    • B01D53/508—Sulfur oxides by treating the gases with solids
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/46—Removing components of defined structure
    • B01D53/68—Halogens or halogen compounds
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J15/00—Arrangements of devices for treating smoke or fumes
    • F23J15/02—Arrangements of devices for treating smoke or fumes of purifiers, e.g. for removing noxious material
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J2215/00—Preventing emissions
    • F23J2215/30—Halogen; Compounds thereof

Definitions

  • the invention relates to a method for separating gaseous pollutants, such as hydrogen chloride, hydrogen fluoride, and sulfur oxide, from flue gases, in particular from waste incineration plants by reaction with and binding to dusty additives, such as quicklime (CaO) or calcium carbonate (CaCo 3 ), in which the additives be placed behind the furnace in the flue gas stream, and also has a separating system for performing the process.
  • gaseous pollutants such as hydrogen chloride, hydrogen fluoride, and sulfur oxide
  • dusty additives such as quicklime (CaO) or calcium carbonate (CaCo 3 )
  • the additives be placed behind the furnace in the flue gas stream, and also has a separating system for performing the process.
  • the invention aims to optimize the separation of pollutants from flue gases, in particular from flue gases from waste incineration plants, and has The task is to provide a method and a system which can be implemented with relatively little technical effort and can also be easily adapted to the different operating conditions of different smoke gas generators.
  • the solution to this problem is basically achieved in a method of the generic type in that the additives are introduced at several successive locations in a cascade manner into essentially upwardly directed sections of the flue gas stream and are then separated from the flue gas stream again behind essentially horizontal flow paths by eddy formation in that the separated additives are collected below the vortex sections and then re-entered into the flue gas stream of the previous cascade.
  • a further feature of the process, which is essential to the invention, is that the additives are introduced into the individual cascades in countercurrent to the flue gases and fresh additives are preferably introduced into the last cascade, while the enriched additives are withdrawn behind the first cascade.
  • the reaction of the flue gases with the additives takes a particularly favorable course if the additives are introduced concentrically into the flow paths of the flue gas. However, it is also possible to introduce the additives laterally into the flow paths. Both measures ensure thorough mixing of the flue gas with the additives. Also, the additives are preferably at a temperature of about 300 ° C (573 0 K) are brought to the flue gases to the action, because in this temperature range, the best reaction conditions are created.
  • the additives into the flue gas at a concentration of 100 to 500 g / m. If you go z. B. from a hydrogen chloride content of 3 g / m flue gas results in a stoichiometric ratio of 4o to 200.
  • a separating system for carrying out the method according to the invention is mainly characterized by a plurality of pipe cascades connected in series in the flow direction of the flue gases and having at least one upward flow path, which are connected by intermediate cyclone separators and by metering pipes for additives projecting into each of the upward flow paths of the pipe cascades , wherein the metering tube protruding into one of the tube cascades, preferably into the last tube cascade, is connected via a metering lock to a storage container for fresh additives, while the metering tubes of the first to penultimate Pipe cascades are each connected to the outlet of the next upper pipe cascade downstream cyclone separator, preferably via a lock.
  • the outlet of the cyclone separator downstream of the first pipe cascade is coupled via a lock to a conveyor system, preferably a compressed air conveyor, which is connected to a storage container, which in turn is preferably assigned to the metering pipe of the last pipe cascade.
  • a conveyor system preferably a compressed air conveyor
  • the metering tube downstream of the storage container can be connected via a fork tube on the one hand to the metering lock of the storage container for fresh additives and on the other hand to a metering lock of the storage container for the enriched additives.
  • the storage container for the enriched additives in addition to the metering lock with a further trigger element, preferably with a trigger slide or metering lock.
  • the metering locks can be formed by cellular wheel locks or double pendulum flaps, which, due to their mode of operation, prevent smoke gases from reaching the storage containers and / or the collecting spaces of the cyclone separator through the metering tubes.
  • cyclone separators downstream of the first to penultimate pipe cascade are working cyclones (reactors), while the cyclone separator downstream of the last pipe cascade is a pure separator cyclone.
  • This separator system has several, namely at least three pipe cascades 1, 2 ... 3, which are in flow connection with each other through intermediate cyclone separators 4 ... 5, which form working cyclones, while the uppermost pipe cascade in the exemplary embodiment, the pipe cascade 3, into a pure one Separation cyclone opens.
  • the lower pipe cascade 1 is connected to a flue gas supply line 7, while a suction 8 is connected to the immersion pipe 9 of the separating cyclone 6.
  • Each of the tube cascades 1, 2 ... 3 has an essentially vertical flow path 1 ', 2', 3 ', to which an Pipe elbow 1 ", 2", 3 "connects, which in turn opens into the raw gas inlet 4 ', 5', 6 'of the cyclone separators 4, 5, 6.
  • the separating plant is expediently constructed in such a way that the upward flow paths 1 ', 3' of the odd-numbered pipe cascades 1 and 3 with the cyclone separators 5 downstream of the even-numbered pipe cascades 2 and the upward flow paths 2 'of the even-numbered pipe cascades 2 with the odd-numbered pipe cascades 1 and 3 downstream cyclone separators 4 and 6 are arranged in the vertical alignment.
  • the outlet 4 ′′ of the cyclone separator 4 is connected at its lower end to a lock 12, for example a cellular wheel lock or a double pendulum flap, which is followed by a compressed air conveyor 13.
  • a lock 12 for example a cellular wheel lock or a double pendulum flap, which is followed by a compressed air conveyor 13.
  • the outlet 5 ′′ of the cyclone separator 5 is connected at its lower end to a lock 14, which can also be formed by a cellular wheel lock or a double pendulum flap is and coaxial to their upward directed flow path 1 'is arranged.
  • the lower end of the metering tube 15 is at a certain distance from the lower end of the upward flow path 1 '.
  • the outlet 6 "of the cyclone separator 6 is also connected at its lower end to a lock 16, which in turn can be a cellular wheel lock or a double pendulum flap and works together with a metering tube 17 which is guided vertically into the tube cascade 2.
  • the metering tube 17 also extends coaxial to the upward flow path 2 'of the tube cascade and protrudes down to a point which is at a certain distance from the lower end of the dip tube 1o.
  • a metering tube 18 is arranged coaxially to the upward flow path 3 ′ of the tube cascade 3, the lower end of which is at a certain distance from the lower end of the immersion tube 11 in the cyclone separator 5.
  • metering tube 18 Above the metering tube 18 is a fork tube 19, the branch 19 'of which is connected to a metering lock 20 and the branch 19' 'of which is connected to a metering lock 21.
  • metering locks 2o and 21 can also be designed as cellular wheel locks or double pendulum flaps.
  • the metering lock 2o is connected to the outlet funnel of a storage container 22, in which, for example, fresh cold fired (CaO) or potassium carbonate (CaC0 3 ) is filled.
  • a storage container 22 in which, for example, fresh cold fired (CaO) or potassium carbonate (CaC0 3 ) is filled.
  • the cellular wheel sluice 21 is connected to an outlet funnel 23 of a storage container 24, which also has a further outlet funnel 25.
  • the two discharge funnels 23 and 25 are assigned to the storage container 24 so that they can only be loaded from a partial cross section of the storage container 24.
  • a discharge pipe 26 adjoins the outlet funnel 25, which can optionally be opened or closed via a slide 27. Instead of the slide 27, a free outlet or a metering lock can also be provided.
  • the reservoir 24 is connected to the compressed air conveyor 13 via a pipeline 25.
  • the suction flue 8 forces the flue gas flowing into the flue gas supply line to a certain flow rate, which it maintains on its way through the pipe cascades 1, 2 ... 3 and the cyclone separators 4, 5 ... 6.
  • each of the metering tubes 15, 16, 18 quicklime or calcium carbonate is introduced into the tube cascades in quantities determined by the individual metering locks 20 and / or 21 so that it is distributed as evenly as possible in the flue gas stream.
  • the flue gas reacts with the additives in such a way that, for example, the chlorine contained therein attaches to the additives and is bound by them.
  • the metering locks 2o and / or 21 are set so that the additives in the flue gas reach a concentration between 100 and 500 g / m and are therefore in a stoichiometric ratio of 40 to 200.
  • the reaction of the flue gases with the additives takes place on the one hand in the individual pipe cascades 1, 2 ... 3 and on the other hand also in the intermediate cyclone separators 4 and 5, i. H. the cyclone separators 4 and 5 form so-called working cyclones or reactors.
  • the last cyclone separator 6 arranged in the flow direction of the flue gases primarily has the task of separating the additives contained in the flue gases as soon as the flue gases leave the last pipe cascade 3.
  • the additives (quicklime and / or calcium carbonate) are present at several successive locations in the form of cascades, namely within the tube cascades 1, 2 ... 3 in essentially upward sections 1 ', 2' ... 3 'of the flue gas flow must be entered. Subsequently, these additives are then separated from the flue gas stream behind essentially horizontal flow sections 1 ", 2" ... 3 "by vortex formation in the cyclone separators 4, 5 ... 6. The separated additives are thereby discharged via the outlets 4" , 5 "... 6".
  • Fresh additives from the storage container 22 are introduced into the last tube cascade 3 via the metering lock 20 and the metering tube 18 and, at the same time, additives which have already been enriched can also reach a certain partial quantity from the storage container 24 via the metering lock 21 and the metering tube 18 into the tube cascade 3.
  • the additives separated from the flue gas behind the pipe cascade 3 in the cyclone separator 6 are again introduced into the previous pipe cascade into the pipe cascade 2 in the exemplary embodiment shown, via the metering lock 16 and the metering pipe 17.
  • the cascade-like structure of the separation system makes it possible in a simple manner to adapt it to different practical requirements, simply by varying the number of pipe cascades and cyclone separators connected in series in the flow direction of the flue gases.
EP79103191A 1978-09-12 1979-08-29 Installation pour l'élimination de substances gazeuses nocives des gaz de combustion Expired EP0008770B1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE2839541 1978-09-12
DE19782839541 DE2839541A1 (de) 1978-09-12 1978-09-12 Verfahren zur abscheidung von gasfoermigen schadstoffen, wie chlorwasserstoff, fluorwasserstoff und schwefeloxyd, aus rauchgasen, insbesondere von muellverbrennungsanagen, sowie abscheideanlage zur durchfuehrung des verfahrens

Publications (2)

Publication Number Publication Date
EP0008770A1 true EP0008770A1 (fr) 1980-03-19
EP0008770B1 EP0008770B1 (fr) 1981-12-30

Family

ID=6049196

Family Applications (1)

Application Number Title Priority Date Filing Date
EP79103191A Expired EP0008770B1 (fr) 1978-09-12 1979-08-29 Installation pour l'élimination de substances gazeuses nocives des gaz de combustion

Country Status (5)

Country Link
EP (1) EP0008770B1 (fr)
JP (1) JPS5539298A (fr)
BR (1) BR7905792A (fr)
DE (2) DE2839541A1 (fr)
DK (1) DK150704C (fr)

Cited By (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0040857A2 (fr) * 1980-05-28 1981-12-02 Deutsche Kommunal-Anlagen Miete GmbH Procédé et dispositif de séparation de produits nocifs gazeux et solides des résidus se dégageant lors des procédés thermiques, plus particulièrement lors de la pyrolyse de déchets
GB2152915A (en) * 1983-11-11 1985-08-14 Steinmueller Gmbh L & C Multi-stage method of binding gaseous harmful substances contained in flue gases
FR2565843A1 (fr) * 1984-06-18 1985-12-20 Geteba Procede et dispositif pour neutraliser des elements acides contenus dans des fumees provenant d'incinerateurs
EP0211483A2 (fr) * 1985-06-13 1987-02-25 Aalborg Ciserv International A/S Réacteur à lit fluidifié et son procédé opérationnel
AT389652B (de) * 1983-03-12 1990-01-10 Cleve Urban Dipl Ing Verfahren zur abscheidung von in rauchgasen enthaltenen gasfoermigen schadstoffen
WO1996021504A1 (fr) * 1995-01-10 1996-07-18 Von Roll Umwelttechnik Ag Procede pour la refrigeration et l'epuration des gaz de fumees
US20130164202A1 (en) * 2011-12-23 2013-06-27 Industrial Technology Research Institute Recirculated-suspension pre-calciner system
EP2614876A3 (fr) * 2012-01-13 2014-12-03 Korea Institute of Energy Research Système à haute pression et à haute température pour la désulfuration et la déshalogènation de gaz
CN104474894A (zh) * 2014-11-20 2015-04-01 王在仕 一种旋风筒烟气干法催化脱硫装置及工艺
US20150157978A1 (en) * 2013-12-11 2015-06-11 Industrial Technology Research Institute Loop tower co2 capture system, carbonator, calciner and operating method thereof

Families Citing this family (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4226831A (en) * 1979-03-16 1980-10-07 Allis-Chalmers Corporation Apparatus for removal of sulfur from gas
DE3218636A1 (de) * 1982-05-18 1983-11-24 Reith Hans Juergen Heizeinrichtung mit abgas-waermepumpe
DE3234796C2 (de) * 1982-09-20 1986-11-13 Dr. Goldberg & Partner Umwelttechnik GmbH, 8000 München Verfahren und Vorrichtung zum Abscheiden von gasförmigen Schadstoffen aus Rauchgasen mittels staubförmiger Additive

Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3093465A (en) * 1959-05-08 1963-06-11 Pan American Petroleum Corp Method for treatment of gases
DE2225686A1 (de) * 1971-05-28 1972-12-14 Tam Verfahren und Vorrichtung zur Adsorption von Fluor und Fluorverbindungen auf Aluminiumoxyd
DE2615828A1 (de) * 1976-04-10 1977-10-13 Heinz Hoelter Verfahren und vorrichtung zur gasreinigung
DE7716772U1 (de) * 1977-05-27 1978-02-16 Hoelter, Heinz, 4390 Gladbeck Vorrichtung zur trockenen gasreinigung
DE2746806A1 (de) * 1976-10-18 1978-04-20 Ricoh Kk Elektrophotographische einrichtung
DE2723958A1 (de) * 1977-05-27 1978-12-07 Heinz Hoelter Verfahren und vorrichtung zur trockenen gasreinigung

Patent Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3093465A (en) * 1959-05-08 1963-06-11 Pan American Petroleum Corp Method for treatment of gases
DE2225686A1 (de) * 1971-05-28 1972-12-14 Tam Verfahren und Vorrichtung zur Adsorption von Fluor und Fluorverbindungen auf Aluminiumoxyd
DE2615828A1 (de) * 1976-04-10 1977-10-13 Heinz Hoelter Verfahren und vorrichtung zur gasreinigung
DE2746806A1 (de) * 1976-10-18 1978-04-20 Ricoh Kk Elektrophotographische einrichtung
DE7716772U1 (de) * 1977-05-27 1978-02-16 Hoelter, Heinz, 4390 Gladbeck Vorrichtung zur trockenen gasreinigung
DE2723958A1 (de) * 1977-05-27 1978-12-07 Heinz Hoelter Verfahren und vorrichtung zur trockenen gasreinigung

Cited By (15)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0040857A3 (en) * 1980-05-28 1982-05-12 Deutsche Kommunal-Anlagen Miete Gmbh Process and apparatus for the separation of gaseous and solid noxious products from residues arising from thermal processes, particularly from the pyrolysis of refuse
EP0040857A2 (fr) * 1980-05-28 1981-12-02 Deutsche Kommunal-Anlagen Miete GmbH Procédé et dispositif de séparation de produits nocifs gazeux et solides des résidus se dégageant lors des procédés thermiques, plus particulièrement lors de la pyrolyse de déchets
AT389652B (de) * 1983-03-12 1990-01-10 Cleve Urban Dipl Ing Verfahren zur abscheidung von in rauchgasen enthaltenen gasfoermigen schadstoffen
GB2152915A (en) * 1983-11-11 1985-08-14 Steinmueller Gmbh L & C Multi-stage method of binding gaseous harmful substances contained in flue gases
FR2565843A1 (fr) * 1984-06-18 1985-12-20 Geteba Procede et dispositif pour neutraliser des elements acides contenus dans des fumees provenant d'incinerateurs
EP0211483A3 (en) * 1985-06-13 1988-09-28 Aalborg Vaerft A/S Fluidized-bed reactor and its operational process
EP0211483A2 (fr) * 1985-06-13 1987-02-25 Aalborg Ciserv International A/S Réacteur à lit fluidifié et son procédé opérationnel
WO1996021504A1 (fr) * 1995-01-10 1996-07-18 Von Roll Umwelttechnik Ag Procede pour la refrigeration et l'epuration des gaz de fumees
CH689633A5 (de) * 1995-01-10 1999-07-30 Von Roll Umwelttechnik Ag Verfahren zur Kuehlung und Reinigung von Rauchgasen.
US20130164202A1 (en) * 2011-12-23 2013-06-27 Industrial Technology Research Institute Recirculated-suspension pre-calciner system
US9610536B2 (en) * 2011-12-23 2017-04-04 Industrial Technology Research Institute Recirculated-suspension pre-calciner system
EP2614876A3 (fr) * 2012-01-13 2014-12-03 Korea Institute of Energy Research Système à haute pression et à haute température pour la désulfuration et la déshalogènation de gaz
US20150157978A1 (en) * 2013-12-11 2015-06-11 Industrial Technology Research Institute Loop tower co2 capture system, carbonator, calciner and operating method thereof
US9610537B2 (en) * 2013-12-11 2017-04-04 Industrial Technology Research Institute Loop tower CO2 capture system, carbonator, calciner and operating method thereof
CN104474894A (zh) * 2014-11-20 2015-04-01 王在仕 一种旋风筒烟气干法催化脱硫装置及工艺

Also Published As

Publication number Publication date
EP0008770B1 (fr) 1981-12-30
DK150704C (da) 1987-11-02
DK362779A (da) 1980-03-13
JPS5539298A (en) 1980-03-19
BR7905792A (pt) 1980-05-20
DE2839541A1 (de) 1980-03-20
DE2961696D1 (en) 1982-02-18
DK150704B (da) 1987-06-01

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